Carbon monoxide conversion catalysts

ABSTRACT

This invention relates to a catalyst, to a process for the manufacture thereof and to a process for manufacturing hydrogen by reacting carbon monoxide with water at 150*-550*C in the presence of the above catalyst. This catalyst comprises an active phase consisting of the mixed oxides of (a) copper and (b) a trivalent metal selected from aluminum, chromium, manganese, iron and cobalt, at least 60% by weight of said mixed oxides having a spinel structure. The catalyst is manufactured by admixing the catalyst components in solution with a heat-decomposable complexing organic compound or with a heat-decomposable gelforming compound, the solvent being evaporated thereafter and the mixture being finally roasted at a temperature of at least 200*C.

United States atent 1191 Sugier 14 1 Jan. 22, 1974 CARBON MONOXIDE CONVERSION CATALYSTS [75] Inventor: Andr Sugier, Ruel Malmaison,

France [22] Filed: July 21, 1970 [21] Appl. No.: 56,974

[30] Foreign Application Priority Data July 25, 1969 France 69.25671 52 us. 0 252/443, 252/454, 252/455 R, 252/458, 252/459, 252/463, 252/465,

51 Int. Cl 2 1;01 1 1 22, 13 1 j 11/06 [58] Field at Search 106/65, 66; 25-2/477 R, 467, 252/471, 443, 454, 463, 474, 476, 465, 466

3,295,918 l/l967 Briggs et aI. 252/471 X 3,296,002 1/I967 Hare 106/65 X 3,326,819 6/1967 Newman 252/471 X 3,342,616 9/1967 Alper et al 106/65 X 3,438,724 4/1969 Hartford et a1. 106/66 X 3,565,646 2/1971 I'IOUSII 106/65 FOREIGN PATENTS OR APPLICATIONS 2,994 1907 Great Britain 106/65 Primary Examiner-Daniel E. Wyman Assistant Examiner-W. J. Shine Attorney, Agent, or Firm-I. William Millen 5 7] ABSTRACT This invention relates to a catalyst, to a process for the manufacture thereof and to a process for manufacturing hydrogen by reacting carbon monoxide with water at l50550C in the presence of the above catalyst. This catalyst comprises an active phase consisting of the mixed oxides of (a) copper and (b) a trivalent metal selected from aluminum, chromium, manganese, iron and cobalt, at least 60% by weight of said mixed oxides having a spine] structure. The catalyst is manufactured by admixing the catalyst components in solution with a heat-decomposable complexing organic compound or with a heat-decomposable gelforming compound, the solvent being evaporated thereafter and the mixture being finally roasted at a temperature of at least 200C.

30 Claims, No Drawings 1 CARBON MONOXlllDE CONVERSION CATALYSTS This invention relates to a process for producing hydrogen from carbon monoxide and water according to the conversion reaction:

C H 0 2 CO H Since this reaction is exothermic, the equilibrium is displaced to the right when the temperature is decreased.

Up to now, two types of catalysts have been used in this reaction, type one used at a high temperature and the other type at a low temperature. The former have but a low activity at the low temperatures; they are rather inexpensive; and their use results in limited conversion rates owing to the unfavorable influence of temperature on the reaction balance. The other catalysts, which are active at a low temperature, are more expensive and weaker since they lose their activity when the temperature is increased too much.

This invention relates to new catalysts which may be used for converting carbon monoxide and steam to hydrogen. These catalysts may be used in a broad temperature range, usually 150 to 450C and even, in particular cases, 150 to 550C, which constitutes a substantial advantage.

These catalysts comprise at least one mixed oxide of formula CulVl O wherein M is a trivalent metal selected from the group consisting of aluminum, chromium, manganese, iron and cobalt, said oxide having, at least partly, a spine] structure.

In contrast to the known catalysts, which contain copper as an active element in the form of copper oxide admixed with other substances or deposited thereon, the catalysts of this invention contain copper associated with other elements in the form of chemical compounds of a well-defined composition and structure. It has unexpectedly been found that copper has an higher activity and a greater stability with respect to the carbon monoxide conversion, when it is part of a defined chemical compound of the spinel type, said compound having the general formula Cu M 0, in which M is a trivalent metal selected from the group consisting of aluminum, chromium, manganese, iron and cobalt.

The present invention also applies to the catalysts whose active phase consists of mixed oxides in which copper is associated with at least two of the hereinbefore disclosed trivalent metals, said mixed oxides being at least partly of the spinel type.

The invention also relates to the catalysts whose active phase consists of mixed oxides in which copper and at least one other bivalent metal selected from the group consisting of magnesium, cobalt and cadmium are associated with at least one of the hereinbefore disclosed trivalent metals, said mixed oxides being at least partly of the spinel type.

The spinel content of the active phase may be determined by X-rays diffraction analysis since the spinels are oxygen-containing chemical compounds of a welldefined composition, i.e. they have a stoichiometric composition, taking into account the lattice defects. Their crystallographic phase is unique and may be characterized easily.

By active phase, there is meant the oxides of the above-mentioned trivalent and bivalent metals, as a whole, including copper, which are present in the catalyst.

It has been found that it was of major importance for the carbon monoxide conversion catalysts that copper be present in the cubic lattice of a spine] to obtain a high activity and, above all, a high stability of the catalysts. Copper must be located either in a tetrahedral system, in the case of a normal spine], or in a octahedral system, in the case of an inverted spinel.

It is thus preferred that the active phase have the highest possible spinel content. The most preferred catalysts have an active phase whose spinel content is at least by weight.

The catalysts of this invention may be supported if desired. In that case, the carrier may be of any type known in catalysis, the preferred carriers having a substantial pore volume, for example at least 20 cubic centimeters per 100 grams of carrier.

For example, alumina, silica, silica-alumina, magnesia, silica-magnesia, metal aluminates and silicium carbide may be used as carriers.

A preferred carrier consists of alumina balls or extrudates of 2-5 millimeters length, said balls or extrudates having a specific surface of 100 to 350 sq. meters per gram and a pore volume of 40 to ccm per grams.

Another object of this invention is the manufacture of the thus defined catalysts. As a matter of fact, it has been found that the process for manufacturing spinels do not all result in the same products and that, for example, the catalysts obtained by fritting oxides at a high temperature were less active than those obtained at a moderate or low temperature.

A known process for manufacturing mixtures of metal oxides which may be used at a low temperature consists of co-precipitating the hydroxides of the metals to be associated, either by adding a convenient chemical compound to a solution of the salts of these metals, or by adding such a solution to a solution of the said compound, and thereafter decomposing the obtained hydroxide mixture. However this method does not result in a sufficiently homogeneous mixture because a perfect coprecipitation cannot be obtained easily. One other disadvantage results from the use of, for example, sodium hydroxide or sodium carbonate as precipitating agent instead of ammonia when the hydroxides, for example copper hydroxide, are partly or completely soluble in ammonia. A careful washing of the hydroxides must follow since sodium is quite detrimental to the activity of such catalysts.

For manufacturing unsupported catalysts, this invention makes use of methods starting from a precursor containing the metal elements in a proportion substantially corresponding to the composition of the spinel phase. These precursors may be manufactured by a process which comprises admixing a gel-forming compound or a complexing compound to a solution of the metal ions to be associated in any convenient form, said compounds being heat-decomposable, preferably without residue. Thus a stable solution of the metal ions to be associated is manufactured and the solvent is removed thereafter without settling of the metal ions, which results in an extremely viscous composition which may be decomposed by heat.

To obtain an homogeneous mixed oxide, it is of major importance to avoid any segregation of the metal compounds in the solution and any separation of crystallized compounds; it is also important to obtain a solution of sufficiently high viscosity to avoid any further separation of the elements during the decomposition. The elements to be associated in the precursor may be used as soluble salts which decompose under the conditions of manufacture to the final oxide, for example as nitrate, nitrite, sulfate, sulfite, thiosulfate, chloride, chlorate, chlroite, hypochlorite, perchlorate, carbonate, formate, acetate, propionate, methylate, ethylate, isopropylate, propylate or oxalate. Salts of acids containing one of the elements to be associated may also be used, for example chromates or bichromates. Finally an anhydride, an acid or a hydroxide in solution may also be used.

The salts may be dissolved either in a neutral, basic or acid aqueous solution or in a liquid other that water, for example a conventional solvent.

When a gel-forming substance is added to this solution, the obtained product consists of a perfectly homogeneous and transparent gel. The latter may be subjected to decomposition by heating at a temperature higher than 200C, preferably 300 to 660C. The oxides are obtained in the form of a very fine powder.

It must be pointed out that the gel results from a mechanism quite different from that conventionally employed in the manufacture of catalysts, wherein an alumina or silica gel, or a gel obtained from other metal hydroxides, either pure or intermixed, is added to a solution containing other elements: in the latter case, indeed, the gel-forming agent remains in the final product in the form of an oxide combined with the other oxides or intimately admixed therewith.

According to this invention, any substance which, when added to the metal salts solution, substantially increases the viscosity thereof, may be used as a gelforming compound. By way of example, there will be used a gum, for example gum adraganth, senegal gum, shellac, gum Dammar, Carouba gum, or a gel-forming or thickening substance, for example, alginic acid, an alignate, a polyvinyl alcohol, a urea-formaldehyde resin, a carboxyvinyl polymer, a polyethylene oxide, carboxy methylcellulose, methyl cellulose, a polyglycol, a polymethacrylate, a polyethanolamine, an oxide wax or a glue. The gel-forming substance may be selected in view of its stability in the presence of the ions which may be present in the solution. Senegal gum and gum adraganth give the best results.

When a complex-forming substance, which is able to decompose by heat, is added to a solution containing the metal elements to be associated, said substance may be selected from the group consisting of the polycarboxylic acids, the acids-alcohols, the acids-amines, the ketoacids and their salts. Said substance is used in an amount lower than 0.] gram-equivalent, preferably 0.002 to 0.1 gram-equivalent, per gram-equivalent of the metal to be complexed.

Tartaric acid and citric acid, both aliphatic hydroxy carboxylic acids, may be used with benefit.

The resulting solution may be concentrated by vaporization, thus resulting in a very viscous homogeneous liquid or an amorphous solid which may be subjected to heat decomposition at a temperature higher than 200C, preferably between 300 and 660C.

The thermal decomposition of the precursor to an oxide may be carried out either directly or after drying. In that case, the drying may be carried out under reduced pressure or at any pressure, in the presence of air or any other gas. The thermal decomposition is itself carried out in air or in a reducing, oxidizing or neutral atmosphere.

A supported catalyst may be manufactured by impregnating a carrier such as defined heretofore by a method resulting in the formation of a spinel phase on the carrier from a mixed oxide precursor containing the metal elements to be associated in proportions substantially corresponding to the desired spinel phase.

The mixed oxide precursor may be obtained according to any one of the hereinbefore given methods for manufacturing unsupported catalysts.

Two embodiments may be used: a gel-forming subtance or a complexing substance may be added to a solution of the metal compounds to be associated, which results in a precursor that may be used to impregnate the carrier. Alternatively the gel forming substance or the complexing substance may be admixed with the carrier, and, after drying thereof, a solution of the metal compounds to be associated is added thereto.

The mixed oxide precursor which has thus been admixed with the carrier is thereafter subjected to thermal decomposition under the hereinbefore given conditions.

One further object of this invention is a processs for producing hydrogen from carbon monoxide and water, said process comprising the use as catalyst of one of the hereinbefore defined compositions.

These catalyst compositions, which possess a high stability and a great activity, may be used in a broad temperature range, for example from 150 to 450C and even 150 to 550C when more than two metal elements are present.

The following examples are given for illustrative purposes and must not be considered as limiting the scope of the invention Examples 1A, 18, 5A and 9A are given for comparative purposes.

In these examples, the catalyst activity was determined as follows: the catalyst was introduced into a tubular oven of 20 mm diameter, said oven being maintained at a constant temperature under atmospheric pressure: a gaseous mixture of 20 by volume of carbon monoxide and by volume of hydrogen, together with steam in a ratio of 1 part by volume of steam per part by volume of gas, was passed therethrough. The hourly feed rate by volume (hourly volume of feed per volume of catalyst) was, except if otherwise states, 2,000 liters per liter of catalyst and per hour.

The gas was analyzed at the reactor outlet and the converted carbon monoxide was determined as follows:

Percent conversion No. of mols of CO at inletNo. of mols of CO at outlet No. of mols of CO at inlet Examples 1 to 9 were given for illustrating the manufacture and the use of the unsupported catalysts.

EXAMPLE 1 CuCR O spinel hi riiis product was thereafter 'heated for l hour at400C in a gas stream of 98% nitrogen and 2 hydrogen. It was finally shaped to agglomerates of 5 mm diameter.

-L TABLE l Example Temperature CO conversion "C after 1 hour after hours after 100 hours I 220 97 95 94 l A 220 88 74 60 l B 220 87 60 30 2 220 93 92 9O 3 240 9] 90 89 4 220 97 95 94 EXAMPLE 1 A The catalysts of examples 1 to 4 have been heated to 120.8 g of Cu(NO 31-11 0 and 400.1 g of Cr(NO,,) 9 H O have been dissolved in their water of crystalliza-I tion and heated in air at 450C for 90 minutes. An? X-ray analysis has shown that the manufactured sample consisted essentially of Cr O and CuO with a small amount of Cu Cr O.,. The product was then heated for. 1 hour at 300C in a gas stream of 98 nitrogen and 2% hydrogen. It was finally shaped to agglomerates of 5 mm diameter.

EXAMPLE 1 B 120.8 g of Cu(NO 3 H O have been heated at 450c for 90 minutes in air and thus transformed to; CuO; the latter was heated at 300C for 90 minutes in the same gas stream as in example 1 and finally shaped to agglomerates of 5 mm diameter.

EXAMPLE 2 Four hundred and four g of Fe (N09 9 H O have; been admixed with 55.25 g of CuCO Cu(Ol-l) and 300 ml of water were added thereafter. The mixture was heated up to 80C; once CO, was evolved, 60 g of gum adraganth were added slowly under constant and; 40 efficient stirring.

The resulting gel was heated at 450C in air for 2i hours. The X-ray analysis showed a substantially pure CuFe O phase.

After heating at 400C for 90 minutes in a gas stream: of 98 N and 2 H the product was shaped to agglomerates of 5 mm diameter and 5 mm height. 5

EXAMPLE 3 375.1 g of Al(NO 9 H 0 have been admixed with@ 55.25 g of CuCO Cu (OH): and 300 ml. of water added thereto. The mixture was heated at 80C and; when the gas evolution was terminated 60 g of gum adraganth were added to the well-stirred solution. 1

The dehydrated product was heated in air at 650C for 2 hours, thus resulting in the Cu A1 0, phase.

Mm EXAMPLE 4 420C for 24 hours in a gas stream of 4 H and 96 nitrogen. They were used thereafter under the same conditions as before: their activity loss with respect to the carbon monoxide conversion reaction after these 24 hours was lower than 2 EXAMPLE 5 49.8 g of copper carbonate CuCO Cu(OH) and 8.6 g of cadmium carbonate CdCO were caused to dissolve in 150 ml of an aqueous solution of 100 g CrO; 'in water. 20 g of gum adraganth were added thereto, so

as to form a homogeneous gel of high viscosity.

EXAMPLE 5 A Example 5 was repeated, except that gum adraganth was omitted.

EXAMPLE 6 49.8 g of copper carbonate CuCO Cu(Ol-l) and 4.2 g of magnesium carbonate MgCO have been caused to dissolve in 150 ml of an aqueous solution of 80 g of chromic anhydride CrO and 75 g of aluminum nitrate Al(NO 9H O. 40 g of Senegal gum were slowly added thereto, so as to form a gel of high viscosity.

EXAMPLE 7 49.8 g of copper carbonate CuCO Cu(OH) and 4.7 l

"g of copper hydroxide were caused to dissolve in 150 ml of an aqueous solution of 100 g chromic anhydride C10 Forty g of gum adraganth were slowly added thereto I under constant stirring, thus resulting in a homogeneous gel of high viscosity.

EXAMPLE 8 49.8 g of copper carbonate CuCO Cu(OH) and 8.6 g of cadmium carbonate CdCO have been dissolved in 170 ml of an aqueous solution of g chromic anhydride CrO and 80.8 g iron nitrate Fe(NO 91-1 0.

Forty g of Senegal gum were added thereto.

The products of examples 5 to 8, which are catalyst precursors, have been dried at 120C for 4 hours, then 0 subjected to decomposition by heating at 550C in an air stream for 4 hours. The resulting powders have been shaped to particles of 3 mm diameter and 3 mm height, and then heated at 300C for 12 hours in a gas mixture of 97 by volume of nitrogen and 3 by volume of hydrogen.

' Table II summarizes the results obtained with the alysts of examples 5 to 8 after 2 hours and hours, at the given temperatures. The third column (T 220C) summarizes the results obtained with the same catalysts after 24 hours heating at 550C. in a gas stream of 4 by volume of hydrogen and 96 by volume of nitrogen.

49.8 g of copper carbonate CuCO Cu(Ol-l) and 6.4 g of cadmium oxide CdO have been dissolved in 170 ml of an aqueous solution of 80 g of chromic anhydrid and 1 50.2 g of manganese nitrate Mn(NO 4 H 0. 8 g of tartaric acid were added thereto Alumina of 2-5 mm size and with a pore volume of 70 cm per 100 g, whereof cm of macropore volume, have been inpregnated with the above solution.

8 marmfig'ms'sannae'heatea 111311 at 550C for 4 hours. v

EXAMPLE 11 It gives the spinel content of the active phase, said 5 375.1 g of aluminum nitrate Al(NO 9 H 0 and content being determined by X-rays analysis. It also 55.25 g of copper carbonate CuCO Cu(OH) have gives the stability thereof as determined by the by been dissolved in 200 ml of water at 80C. 6 g of gum weight of copper which dissolves when a catalyst samadraganth have been added thereto. tple gs }admixed with nitric ac1d of density 1.38 at C 10 Silica extrudates having a pore volume of ccm p51 or ours. .100 grams have been mpregnated twice with this solu- TABLE 11 Samples Percent by weigh "if all l ei'oent CO conversion of spinel in Percent copper o the act 105 "tit. T 9 ..i:: f99. i:i::. .111; Hi LE 1.. phase after after after after after after 2h 10011 2h 10011 2h 10011 @5513; 9 to 12 are given for illustrat ing 0185565; 151; at 8 0C "i113 impregnations being separated by a ture and use of supported catalysts. drying step.

The resulting product has been roasted at 550C for EXAMPLE 9 4 hours in an air stream.

Six g of citric acid are added to 150 ml of an aqueous 30 solution of g chromic anhydride CrO and 55.2 g EXAMPLE 12 copper carbonate CuCO Cu(OH)- This solution is Two hundred twenty five g of aluminum nitrate Al(- used to impregnate in two steps with intermediate dry- N09 9 H O, 161.6 g of iron nitrate Fe (N09 9 H O ing alumina balls of 2-5 mm size, 50 ccm per 100 gram and 55.2 g of copper carbonate CuCO Cu(OH) have pore volume and 350 m /g specific surface. 35 been dissolved in 100 ml of water at 80C. After com- The impregnated balls have been heated in air at plete dissolution, 10 g of citric acid have been added t- 550C for 4 hours. The catalyst was finally tested at a hereto. This solution has been used to impregnate in VVl-l of 1500 h". -two steps with intermediate drying, silicon carbide balls of 2-5 mm size and 45 ccm per 100 g pore volume. EXAMPLE 9 A 0 Then the balls have been heated at 550C in air for 4 Example 9 was repeated except that no citric acid hours. was used. The catalyst was heated for 4 hours at 450C Table III summarizes the main characteristics of the and tested under the conditions of example 9. catalysts according to examples 9 to 12:

by weight of active phase and carrier EXAMPLE 10 45 by weight of spinel in the active phase copper loss after 5 hours treatment with nitric acid of specific gravity 1.38 at 30C.

It also summarizes the results obtained at 220C and 400C. The third column of results (T 220C) s'ummarizes the results obtained with the catalysts after 24 hours treatment at 550C in a gas stream consisting of 4 by volume of hydrogen and 96 by volume of nitrogen.

TABLE III by weight k by weight 7: copper 72 CO conversion Samples of active of spinel in loss T 220C T 400C T 220C phase the active after after after after after after 2h l00h 2h l00h 2h lOOh phase 9 40 92 9 94 90 90 85 92 88 9A 40 30 73 87 83 82 36 l9 l5 10 38 91 10 93 89 89 86 91 87 l l 32 85 12 93 88 89 81 91 86 2 38 89 l 1 9| 87 88 82 89 85 What we claim is: 1. A shaped particulate agglomerated catalyst consisting essentially of a mixed oxide of (a) copper andv (b) at least one trivalent metal selected from the group consisting of aluminum manganese, iron and cobalt, at least 60 by weight of said mixed oxide having a spine] structure.

2. A catalyst according to claim 1, wherein said mixed oxide essentially has the spinel structure.

3. A catalyst according to claim 1, said mixed oxide further comprising at least one bivalent metal selected from the group consisting of magnesium, cobalt and cadmium.

4. A catalyst according to claim 3, wherein said mixed oxide essentially has the spinel structure.

5. A catalyst consisting essentially of particulate carrier material impregnated with an active phase consisting essentially of a mixed oxide of (a) copper and (b) at least one trivalent metal selected from the group consisting of aluminum, manganese, iron and cobalt, at least 60% by weight of said mixed oxide having a spinel structure.

6. A catalyst as claimed in claim 5, wherein said mixed oxide essentially has the spinel structure.

7. A catalyst as claimed in claim 5, wherein said carrier material is alumina.

8. A catalyst as claimed in claim 5, wherein said carrier material is silica.

9. A catalyst as claimed in claim 5, wherein said carrier material is silicon carbide.

10. A catalyst as defined by claim 3, further compris-' ing particulate carrier material impregnated with said mixed oxide active phase.

11. A catalyst as claimed in claim 10, wherein said mixed oxide essentially has the spinel structure.

12. A catalyst as claimed in claim 10, wherein said carrier material is alumina.

13. A catalyst as claimed in claim 10, wherein said carrier material is silica.

14. A catalyst as claimed in claim 10, wherein said carrier material is silicon carbide.

15. A process for manufacturing a shaped particulate agglomerated catalyst, said process comprising forming a solution containing (a) a dissolved copper compound selected from the group consisting of salts and hydroxides thereof and (b) a dissolved compound of a trivalent metal selected from the group consisting of alumina, chromium, manganese, iron and cobalt, said compound being a salt, anhydride, acid, or hydroxide; admixing to said solution a thermally decomposable gel-forming compound to obtain a homogeneous and transparent gel; heating the resultant gel up to at least 200C to decompose the same and form a finely divided powder of a mixed oxide having at least 60% by weight of the spinel structure; and shaping said finely divided powder to agglomerate.

16. A shaped particulate agglomerated catalyst as I produced by the process of claim 15.

17. A process for producing a catalyst supported on a carrier selected from the group consisting of alumina, silica, silica-alumina, magnesia, silica-magnesia, metal aluminate, and silicon carbide, said process comprising contacting said carrier with a thermally decomposable gel-forming compound or complexing aliphatic hydroxy carboxylic acid and a solution of (a) a dissolved copper compound selected from the group consisting of salts and hydroxides thereof and (b) a dissolved.

compound of a trivalent metal selected from the group consisting of aluminum, chromium, manganese, iron and cobalt, said compound being a salt, anhydride, acid, or hydroxide, evaporating solvent from the thus impregnated carrier, and heating the carrier up to at least 200C to obtain a supported catalyst having a active phase of mixed oxide having at least 60% by weight of a spinel structure.

18. A supported catalyst as produced by the process of claim 17.

19. A process as defined by claim 15, said solution further containing a dissolved compound of a divalent metal selected from the group consisting of magnesium, cobalt and cadmium. I

20. A shaped particulate agglomerated catalyst as produced by the process of claim 19.

21. A process as defined by claim 17, said solution further comprising a dissolved compound of a divalent metal selected from the group consisting of magnesium, cobalt and cadmium.

22. A supported catalyst as produced by the process of claim 21.

23. A process for manufacturing a shaped particulate agglomerated catalyst, said process comprising fonning a solution containing (a) a dissolved copper compound selected from the group consisting of salts and hydroxides thereof and (b) a dissolved compound of a trivalent metal selected from the group consisting of aluminum, chromium, manganese, iron and cobalt, said compound being a salt, anhydride, acid or hydroxide; admixing to saidsolution a thermally-decomposable complex-forrning aliphatic hydroxy carboxylic acid, and concentrating the resulting solution to form a concentrate which is either viscous, homogeneous liquid or an amorphous solid; heating said concentrate up to at least 200C. to decompose the same and form a finely divided powder of a mixed oxide having at least 60% by weight of the spinel structure; and shaping said finely divided power to agglomerate.

24. A shaped particulate agglomerated catalyst as produced by the process of claim 23.

25. A process as defined by claim 23, said solution further containing a dissolved compound of a divalent metal selected from the group consisting of magnesium, cobalt, and cadmium.

26. A shaped particulate agglomerated catalyst as produced by the process of claim 25.

27. A process as defined by claim 23 wherein said aliphatic hydroxy carboxylic acid is nitric or tartaric acid.

28. A shaped particulate agglomerated catalyst as produced by the process of claim 27.

29. A process as defined by claim 27 said solutionfurther containing a dissolved compound of a divalent metal selected from the group consisting of magnesium, cobalt and cadmium.

30. A shaped particulate agglomerated catalyst as produced by thev process of claim 29.

UNITED STATES PATENT OFFICE CERTIFICATE OF CQRRECTION Patent No. 3 787 33 2 Dated January 22 19'74v Inventor(s) An Sugier I I I V I Itis certified that error appears in the above-idntifidta'tent and that said Letters Patent are hereby corrected as shown below:

IN THE HEADING The Address for I the Assignee of Record should read wRueil Malmaison (Hauts de Seine) FRANCE IN THE CLAIMS: Claim 15, Columns9, line 7 ofdthe c1aim= "alumina" should read aluminum v Q I Claim 1, Column 9 line 4 of the Claim:

Insert a comma i after "aluminum".

Signed, and sealed this 2nd day' of July 1974.

' (SEAL) Attest:

EDWARD M. FLETCHERJR. C.MARSHALL DANN Attesting Officer Commissioner of Patents FORM Po-1oso (10-69) v USCOMWDC 5 37 .p59

U.S. GOVERNMENT PRINTING OFFICE: 1959 0-355-334. 

2. A catalyst according to claim 1, wherein said mixed oxide essentially has the spinel structure.
 3. A catalyst according to claim 1, said mixed oxide further comprising at least one bivalent metal selected from the group consisting of magnesium, cobalt and cadmium.
 4. A catalyst according to claim 3, wherein said mixed oxide essentially has the spinel structure.
 5. A catalyst consisting essentially of particulate carrier material impregnated with an active phase consisting essentially of a mixed oxide of (a) copper and (b) at least one trivalent metal selected from the group consisting of aluminum, manganese, iron and cobalt, at least 60% by weight of said mixed oxide having a spinel structure.
 6. A catalyst as clAimed in claim 5, wherein said mixed oxide essentially has the spinel structure.
 7. A catalyst as claimed in claim 5, wherein said carrier material is alumina.
 8. A catalyst as claimed in claim 5, wherein said carrier material is silica.
 9. A catalyst as claimed in claim 5, wherein said carrier material is silicon carbide.
 10. A catalyst as defined by claim 3, further comprising particulate carrier material impregnated with said mixed oxide active phase.
 11. A catalyst as claimed in claim 10, wherein said mixed oxide essentially has the spinel structure.
 12. A catalyst as claimed in claim 10, wherein said carrier material is alumina.
 13. A catalyst as claimed in claim 10, wherein said carrier material is silica.
 14. A catalyst as claimed in claim 10, wherein said carrier material is silicon carbide.
 15. A process for manufacturing a shaped particulate agglomerated catalyst, said process comprising forming a solution containing (a) a dissolved copper compound selected from the group consisting of salts and hydroxides thereof and (b) a dissolved compound of a trivalent metal selected from the group consisting of alumina, chromium, manganese, iron and cobalt, said compound being a salt, anhydride, acid, or hydroxide; admixing to said solution a thermally decomposable gel-forming compound to obtain a homogeneous and transparent gel; heating the resultant gel up to at least 200*C to decompose the same and form a finely divided powder of a mixed oxide having at least 60% by weight of the spinel structure; and shaping said finely divided powder to agglomerate.
 16. A shaped particulate agglomerated catalyst as produced by the process of claim
 15. 17. A process for producing a catalyst supported on a carrier selected from the group consisting of alumina, silica, silica-alumina, magnesia, silica-magnesia, metal aluminate, and silicon carbide, said process comprising contacting said carrier with a thermally decomposable gel-forming compound or complexing aliphatic hydroxy carboxylic acid and a solution of (a) a dissolved copper compound selected from the group consisting of salts and hydroxides thereof and (b) a dissolved compound of a trivalent metal selected from the group consisting of aluminum, chromium, manganese, iron and cobalt, said compound being a salt, anhydride, acid, or hydroxide, evaporating solvent from the thus impregnated carrier, and heating the carrier up to at least 200*C to obtain a supported catalyst having a active phase of mixed oxide having at least 60% by weight of a spinel structure.
 18. A supported catalyst as produced by the process of claim
 17. 19. A process as defined by claim 15, said solution further containing a dissolved compound of a divalent metal selected from the group consisting of magnesium, cobalt and cadmium.
 20. A shaped particulate agglomerated catalyst as produced by the process of claim
 19. 21. A process as defined by claim 17, said solution further comprising a dissolved compound of a divalent metal selected from the group consisting of magnesium, cobalt and cadmium.
 22. A supported catalyst as produced by the process of claim
 21. 23. A process for manufacturing a shaped particulate agglomerated catalyst, said process comprising forming a solution containing (a) a dissolved copper compound selected from the group consisting of salts and hydroxides thereof and (b) a dissolved compound of a trivalent metal selected from the group consisting of aluminum, chromium, manganese, iron and cobalt, said compound being a salt, anhydride, acid or hydroxide; admixing to said solution a thermally-decomposable complex-forming aliphatic hydroxy carboxylic acid, and concentrating the resulting solution to form a concentrate which is either viscous, homogeneous liquid or an amorphous solid; heating said concentrate up to at least 200*C. to decompose the same and form a finely divided powder of a mixed oxide having at least 60% by weight of the spineL structure; and shaping said finely divided power to agglomerate.
 24. A shaped particulate agglomerated catalyst as produced by the process of claim
 23. 25. A process as defined by claim 23, said solution further containing a dissolved compound of a divalent metal selected from the group consisting of magnesium, cobalt, and cadmium.
 26. A shaped particulate agglomerated catalyst as produced by the process of claim
 25. 27. A process as defined by claim 23 wherein said aliphatic hydroxy carboxylic acid is nitric or tartaric acid.
 28. A shaped particulate agglomerated catalyst as produced by the process of claim
 27. 29. A process as defined by claim 27 said solution further containing a dissolved compound of a divalent metal selected from the group consisting of magnesium, cobalt and cadmium.
 30. A shaped particulate agglomerated catalyst as produced by the process of claim
 29. 